EP1219646A1 - Verfahren zur anionischen Polymerisation von Styrol - Google Patents
Verfahren zur anionischen Polymerisation von Styrol Download PDFInfo
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- EP1219646A1 EP1219646A1 EP01127601A EP01127601A EP1219646A1 EP 1219646 A1 EP1219646 A1 EP 1219646A1 EP 01127601 A EP01127601 A EP 01127601A EP 01127601 A EP01127601 A EP 01127601A EP 1219646 A1 EP1219646 A1 EP 1219646A1
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- Prior art keywords
- styrene
- polymerization
- alkyl
- process according
- weight
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- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
- C08F12/00—Homopolymers and copolymers of compounds having one or more unsaturated aliphatic radicals, each having only one carbon-to-carbon double bond, and at least one being terminated by an aromatic carbocyclic ring
- C08F12/02—Monomers containing only one unsaturated aliphatic radical
- C08F12/04—Monomers containing only one unsaturated aliphatic radical containing one ring
- C08F12/06—Hydrocarbons
- C08F12/08—Styrene
Definitions
- the invention relates to a process for the homopolymerization of Styrene, optionally together with a polydiene rubber, in Presence of at least one lithium organyl, at least one Metal-II-organyl and at least one aluminum organyl.
- the anionic polymerization usually proceeds very quickly, so a control because of the considerable heat development becomes difficult on a technical scale. If you lower the polymerization temperature, the viscosity increases in particular too much with concentrated solutions. A decrease in Initiator concentration increases the molecular weight of the formed Polymer. A control of the reaction by an appropriate Dilution of the monomers leads to a higher solvent requirement and lower space-time yields.
- Triisobutylaluminium is still the cheapest. At low temperatures, e.g. around 100 ° C TIBA alone is not or only slightly active in polymerization. Even in combination with lithium alkyl it only acts as Retarder is therefore only an additional one, which is essentially inert Component in the reaction mixture. If the alkyl groups from TIBA for coinitiation of anionic polymerization To induce styrene would result in significant cost advantages. This object is the basis of the present invention.
- a Another object of the invention is a technical Scale of rationally feasible process for continuous to develop anionic polymerization with as much as possible small amounts of solvents.
- Lewis bases in general the rate of anionic polymerization in accelerate nonpolar media and the temperature stability of the lower active species. This prevents Lewis bases the effects desired by the retarding additives. Out for this reason the amount of Lewis bases added is up 500 mol%, based on A + B + C, limited.
- DE-A 198 06 774 describes a process for homopolymerization of vinyl aromatic monomers or copolymerization of vinyl aromatic monomers and dienes in the presence of at least one alkali metal organyl, at least one magnesium organyl and at least one aluminum organyl and one Initiator composition for performing the method.
- aluminum organyl include Called TIBA. This Initiator combination is supposed to set the polymerization rate in wide temperature and concentration ranges enable, in particular it should be possible to raise the polymerization temperature.
- the process according to the invention is preferably used for homopolymerization of styrene, but it can be used in amounts of up to 25% by weight can be replaced by conventional comonomers.
- suitable Comonomers are ⁇ -methylstyrene, p-methylstyrene, ethylstyrene, tert-butyl styrene, vinyl toluene, 1,1-diphenylethylene or 1,2-diphenylethylene, butadiene, isoprene, 2,3-dimethylbutadiene, 1,3-pentadiene, 1,3-hexadienes or piperylene or mixtures thereof.
- the polymerization can also be in the presence of 3 to 40, preferably from 5 to 30% by weight, based on the monomers, of a polydiene rubber, e.g. of polybutadiene or a butadiene / styrene block copolymer, be performed.
- a polydiene rubber e.g. of polybutadiene or a butadiene / styrene block copolymer
- Preferred rubbers are Butadiene / styrene two-block copolymers and styrene / butadiene / styrene three-block copolymers, each with separate or smeared Blocks, as well as mixtures of these block copolymers with polybutadiene in a weight ratio of 85:15 to 50:50.
- Suitable lithium organyls A are ethyl, propyl, isopropyl, n-butyl, sec-butyl, tert-butyl, phenyl, diphenylhexyl, Hexamethylenedi, butadienyl, isoprenyl, polystyryllithium or the multifunctional 1,4-dilithiobutane, 1,4-dilithio-2-butene or 1,4-dilithiobenzene, as well as lithium isopropoxylate, lithium ethyl hexanoate and lithium tertiary amylate.
- Suitable metal (II) organyls B are dialkyls, dialcoholates and Alkyl alcoholates of magnesium, calcium, strontium, barium and Zinc, with magnesium and zinc being preferred. Particularly preferred are (n-butyl) (s-butyl) magnesium, and di-n-alkymagnesium compounds, in which the alkyl radicals have 2 to 8 carbon atoms, in particular di-n-butyl magnesium, (n-butyl) (n-octyl) magnesium and (N-butyl (ethyl) magnesium.
- Lewis bases are basically all known from the literature Additives suitable for anionic polymerization. They contain generally at least one O, N, S or P atom, the has a free pair of electrons. Ethers are preferred and amines, e.g. Tetrahydrofuran, diethyl ether, tetrahydropyran, Dioxane, crown ether, alkylene glycol dialkyl ether, e.g.
- the Addition of Lewis bases often leads to an increase in Reaction rate. Their amount is therefore appropriate to be dimensioned so that the reaction speed of the whole Approach is smaller than in an approach without the addition of retarding components is carried out. Used for this less than 500 mol%, preferably less than 200 mol% and in particular less than 100 mol% of the Lewis base, based on A + B + C.
- the polymerization can be carried out in the presence of a solvent be made.
- the solvents are suitable for the anionic polymerization usual aliphatic, cycloaliphatic or aromatic hydrocarbons with 4 to 12 carbon atoms such as pentane, hexane, heptane, cyclohexane, Methylcyclohexane, iso-octane, decalin, benzene, alkylbenzenes such as Toluene, xylene, ethylbenzene or cumene or suitable mixtures.
- the solvent should of course be the process typical have the required high purity. With the invention Initiator combination it becomes possible with proportionate small amounts of solvents to work.
- the polymerization can also be carried out in the presence of up to 10 wt .-% mineral oil, based on monomers become. Paraffins or white oils with boiling points are preferred above 300 ° C. As is well known, these also set the fluidity down from polystyrene.
- the components of the invention are preferred in one used such a ratio that the lifespan of a polymerizable polystyrene solution compared to that a polystyryllithium solution under the same temperature and Concentration conditions is increased. To do this, you determine the time up to which the polymerizable portion of a polystyrene solution in cyclohexane has dropped to half at 100 ° C. This Half-life for a polystyryllithium solution (approx. 3 mmol / l) for example about 3 hours. One with an inventive Initiator mixture started polystyrene solution, the would have the same number of growing chains under these conditions have a longer half-life. Prefers this half-life is more than 20, very particularly preferred more than 50 hours.
- the combination of the metal alkyl initiators A + B + C is preferred in amounts from 0.0001 to 5 mol%, in particular from 0.01 to 1 mol%, based on the monomers, used. It should Molar ratio Li: Me (II) between 1: 0.1 and 1: 3.8 and that Molar ratio Li: Al are between 1: 0.2 and 1: 4.
- the molar ratio Lewis base to lithium should preferably be at least 0.05: 1 and in particular between 0.1: 1 and 10: 1 lie.
- the lithium, magnesium and aluminum alkyls can be together or individually, temporally or spatially added to the monomer mixture become. They are preferred as a premixed initiator composition used.
- the Components in an inert hydrocarbon for example n-hexane, n-heptane, cyclohexane, ethylbenzene, toluene or white oil dissolved and combined as a solvent.
- the metal alkyls dissolved in the hydrocarbons are mixed with each other and the mixture leaves at least 5 minutes ripen at a temperature in the range of 0 to 120 ° C.
- a solubilizer for example diphenylethylene be added to make one of the components fail to prevent this initiator solution.
- Chain terminators are particularly proton-active Substances such as water, alcohols, aliphatic and aromatic carboxylic acids and inorganic acids such as Carbonic acid or boric acid.
- the target products can be homopolymers or copolymers of styrene and mixtures thereof.
- Polystyrene is preferably obtained.
- HIPS impact-resistant polystyrene
- the molecular weights M n can be within wide limits between 1000 to 1000000 g / mol. M n between 20,000 and 200,000 are preferred.
- the method according to the invention can be used in any printing and temperature-resistant reactor can be carried out, it basically backmixing or non backmixing is possible Reactors (i.e. reactors with stirred or Tubular reactor behavior). It can also be different Combinations of such reactors can be used.
- Reactors i.e. reactors with stirred or Tubular reactor behavior. It can also be different Combinations of such reactors can be used.
- the invention The procedure leads depending on the choice of the initiator concentration and composition, the specially applied process flow and other parameters, such as temperature and possibly temperature curve to polymers with high or low molecular weight. Suitable are, for example, stirred tanks, tower reactors, loop reactors as well as tube reactors or tube bundle reactors with or without internals. Internals can be static or moveable internals his.
- the method is preferably carried out continuously. At least part of the turnover is preferred, in particular Sales between 50 and 100% in a non backmixing Reactor or reactor section carried out.
- the polymerization is carried out at temperatures of at least 80 ° C.
- the reaction zone or parts of the reaction zone can also have higher temperatures, for example more than 100 ° C. At least part of the polymerization is preferred 120 ° C without causing a runaway reaction comes.
- a double-walled, 3-1 stirred kettle used with a standard anchor stirrer.
- the reactor was designed for a pressure of 60 bar and with one Heat transfer medium for isothermal polymerization control tempered.
- the stirred kettle was discharged in two consecutive steps switched, stirred and 4 liter tower reactors further promoted.
- the first tower reactor was at an internal temperature operated from 101 ° C.
- Temperature set so that the inside temperature at the end of the first zone was 124 ° C, at the end of the second zone 158 ° C.
- the polymerization mixture was discharged from the tower reactor a mixer with 5 g / h of methanol, then by a pipe piece heated to 260 ° C and via a pressure control valve relaxed in a vacuum pot kept at 25 mbar.
- the melt was discharged with a screw and granulated.
- the solids content at the outlet of the stirred tank was 26% by weight and 58% by weight at the outlet of the first tower reactor. A quantitative conversion was found at the exit of the second tower reactor (solids content approx. 73% by weight).
- Example 4 In the stirred kettle from Example 4, (100 revolutions per minute) continuously 513 g / h styrene, 487 g / h a rubber solution, manufactured according to O.Z. 0050/49155, example 2, and 20 g of an initiator solution metered and at one constant melt temperature of 92 ° C stirred.
- the dosage the initiator solution was adjusted so that the reactor 3.07 mmol / h of Li compound were fed.
- the stirred tank was discharged into a double-jacket tubular reactor with an inner diameter of 29.7 mm and a length conveyed further from 2100 mm.
- the tubular reactor was for one Pressure of up to 100 bar and for a temperature of up to Designed at 350 ° C.
- the tubular reactor was over a in cocurrent led heat transfer medium tempered and the temperature of the Polymerization mixture over three evenly over the reaction route distributed thermocouples determined.
- the temperature of the The heat transfer medium was 104 ° C at the tube reactor inlet.
- the highest temperature of the polymerization solution was at the end of Tube reactor reached with 182 ° C.
- the polymerization mixture 25 g / h of a mixture of methanol, toluene and mineral oil in a ratio of 8: 32: 60% by weight using an HPLC pump added and in a downstream pipe section with a static mixer homogenized.
- the polymer melt was over a throttle valve in a degassing pot kept at 20 mbar relaxed, drawn off with a screw pump, extruded and granulated.
- the material had a yield stress of 28 n / mm 2 , an elongation at break of 27% and a notched impact strength of 14 kJ / m 2 .
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- Chemical & Material Sciences (AREA)
- Health & Medical Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Medicinal Chemistry (AREA)
- Polymers & Plastics (AREA)
- Organic Chemistry (AREA)
- Polymerization Catalysts (AREA)
- Addition Polymer Or Copolymer, Post-Treatments, Or Chemical Modifications (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Transition And Organic Metals Composition Catalysts For Addition Polymerization (AREA)
Abstract
Description
und wobei die Polymerisation in Gegenwart von 5 bis 500 Mol-%, bezogen auf A+B+C, einer Lewis-Base bei Temperaturen oberhalb von 80°C durchgeführt wird.
Bevorzugt ist TIBA.
s-Butyllithium | 1,6 M in Cyclohexan, Fa. Chemetall |
Triisobutylaluminium | (TIBA) 14%ig in Toluol, Fa. Witco |
(n-Butyl)2magnesium | (MAGALA) 10%ig in Heptan, Fa. Akzo Nobel als 7,5:1 molarer Komplex in |
Triethylaluminium |
Vergleichsbeispiel 1BDie Ansätze 1a) und 1b) wurden wiederholt, dabei aber bei der Herstellung der Initiatorzusammensetzung die Magnesiumverbindung und das TMEDA weggelassen.
Mn (g/mol) | Feststoffgehalt (%) | |
Beispiel 1A | 14.950 | 97 |
Beispiel 1B | 89.970 | 100 |
Li : Mg : A1 : THF = 1 : 1 : 0,8 : 1,8
Vergleichsbeispiel 2B
Die Ansätze 2a) und 2b) wurden wiederholt, aber ohne Zusatz der Magnesiumverbindung.
Mn (g/mol) | Umsatz (%) | |
Beispiel 2A | 26.740 | 98 |
Beispiel 2B | 88.050 | 100 |
Vergleichsbeispiel 3B
Die Ansätze 3a) und 3b) wurden wiederholt, aber ohne Zusatz des TMEDA.
Mn (g/mol) | Umsatz (%) | |
Beispiel 3A | 26.800 | 100 |
Beispiel 3B | 53.000 | 100 |
Claims (12)
- Verfahren zur anionischen Polymerisation von Styrol, gegebenenfalls zusammen mit untergeordneten Mengen an Comonomeren, mittels einer Kombination der Metallorganyl-Initiatoren
- A.
- Lithiumalkyl oder -alkoholat
- B.
- Metall-(II)-alkyl oder -alkoholat
- C.
- Aluminiumalkyl oder -alkoholat der Formel A1 R 1 / 2R2 mit R1 = C1-C4-Alkyl und R2 = H, R1 oder -O-C2H5,
- Verfahren nach Anspruch 1, dadurch gekennzeichnet, daß als Komponente A n- oder sec-Butyllithium eingesetzt wird.
- Verfahren nach Anspruch 1, dadurch gekennzeichnet, daß als Komponente B ein Magnesium- oder Zinkdialkyl eingesetzt wird.
- Verfahren nach Anspruch 1, dadurch gekennzeichnet, daß als Komponente B ein C2- bis C8-Di-n-alkylmagnesium, vorzugsweise Di-n-butylmagnesium, eingesetzt wird.
- Verfahren nach Anspruch 1, dadurch gekennzeichnet, daß als Komponente C Triisobutylaluminium (TIBA) eingesetzt wird.
- Verfahren nach Anspruch 1, dadurch gekennzeichnet, daß als Lewis-Base ein Ether, vorzugsweise Tetrahydrofuran, eingesetzt wird.
- Verfahren nach Anspruch 1, dadurch gekennzeichnet, daß die Polymerisation in Gegenwart von 0 bis 500 Gew.-%, bezogen auf die Monomeren, eines Kohlenwasserstoff-Lösungsmittels, vorzugsweise Toluol, Cyclohexan, Heptan, Ethylbenzol und/oder von 0 bis 10 Gew.-% eines Weißöls durchgeführt wird.
- Verfahren nach Anspruch 1, dadurch gekennzeichnet, daß die Polymerisation in Gegenwart von 3 bis 40 Gew.-%, bezogen auf die Monomeren, eines Polydienkautschuks durchgeführt wird.
- Verfahren nach Anspruch 1, dadurch gekennzeichnet, daß die Kombination der Metallorganyl-Initiatoren A+B+C in Mengen von 0,0001 bis 5 Mol-%, bezogen auf die Monomeren, eingesetzt wird.
- Verfahren nach Anspruch 1, dadurch gekennzeichnet, daß das Molverhältnis Li : Me(II) zwischen 1 : 0,1 und 1 : 3,8 und das Molverhältnis Li : A1 zwischen 1 : 0,2 und 1 : 4 liegt.
- Verfahren nach Anspruch 1, dadurch gekennzeichnet, daß das Molverhältnis Lewis-Base : Li mindestens 0,05 : 1 beträgt und vorzugsweise zwischen 0,1 : 1 und 10 : 1 liegt.
- Kontinuierliches Verfahren zur anionischen Polymerisation von Styrol, gegebenenfalls in Gegenwart von 5 bis 30 Gew.-%, bezogen auf Styrol, eines Polydienkautschuks, mittels 0,01 bis 1 Mol-%, bezogen auf Styrol, einer Kombination der Metallorganyl-InitiatorenA. n- oder sec-Butyllithium,B. einem C2-C8-n-Dialkylmagnesium oder (n-Butyl)(sec-Butyl)-magnesium,C. Triisobutylaluminium,
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
DE10065331A DE10065331A1 (de) | 2000-12-27 | 2000-12-27 | Verfahren zur anionischen Polymerisation von Styrol |
DE10065331 | 2000-12-27 |
Publications (2)
Publication Number | Publication Date |
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EP1219646A1 true EP1219646A1 (de) | 2002-07-03 |
EP1219646B1 EP1219646B1 (de) | 2005-11-16 |
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Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
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EP01127601A Expired - Lifetime EP1219646B1 (de) | 2000-12-27 | 2001-11-20 | Verfahren zur anionischen Polymerisation von Styrol |
Country Status (4)
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---|---|
EP (1) | EP1219646B1 (de) |
AT (1) | ATE310030T1 (de) |
DE (2) | DE10065331A1 (de) |
ES (1) | ES2252134T3 (de) |
Cited By (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO2004039855A1 (de) * | 2002-10-28 | 2004-05-13 | Basf Aktiengesellschaft | Verfahren zur anionischen polymerisation von schlagzähem polystyrol |
Citations (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4473661A (en) * | 1982-07-01 | 1984-09-25 | The Firestone Tire & Rubber Company | Polymerization catalyst system containing organolithium, dialkyl magnesium and/or trialkyl aluminum, and a phosphine oxide |
DE19806774A1 (de) * | 1998-02-18 | 1999-08-19 | Basf Ag | Verfahren zur retardierten anionischen Polymerisation |
DE19954818A1 (de) * | 1999-11-13 | 2001-05-17 | Basf Ag | Verfahren zur anionischen Polymerisation von vinylaromatischen Monomeren |
-
2000
- 2000-12-27 DE DE10065331A patent/DE10065331A1/de not_active Withdrawn
-
2001
- 2001-11-20 EP EP01127601A patent/EP1219646B1/de not_active Expired - Lifetime
- 2001-11-20 AT AT01127601T patent/ATE310030T1/de not_active IP Right Cessation
- 2001-11-20 DE DE50108076T patent/DE50108076D1/de not_active Expired - Lifetime
- 2001-11-20 ES ES01127601T patent/ES2252134T3/es not_active Expired - Lifetime
Patent Citations (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4473661A (en) * | 1982-07-01 | 1984-09-25 | The Firestone Tire & Rubber Company | Polymerization catalyst system containing organolithium, dialkyl magnesium and/or trialkyl aluminum, and a phosphine oxide |
DE19806774A1 (de) * | 1998-02-18 | 1999-08-19 | Basf Ag | Verfahren zur retardierten anionischen Polymerisation |
DE19954818A1 (de) * | 1999-11-13 | 2001-05-17 | Basf Ag | Verfahren zur anionischen Polymerisation von vinylaromatischen Monomeren |
Non-Patent Citations (1)
Title |
---|
WELCH F J: "Polymerization of Styrene by n-Butyllithium. II. Effect of Lewis Acids and Bases", JOURNAL OF THE AMERICAN CHEMICAL SOCIETY, AMERICAN CHEMICAL SOCIETY, WASHINGTON, DC, US, no. 82, 1960, pages 6000 - 6005, XP002104542, ISSN: 0002-7863 * |
Cited By (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO2004039855A1 (de) * | 2002-10-28 | 2004-05-13 | Basf Aktiengesellschaft | Verfahren zur anionischen polymerisation von schlagzähem polystyrol |
Also Published As
Publication number | Publication date |
---|---|
ES2252134T3 (es) | 2006-05-16 |
DE10065331A1 (de) | 2002-07-04 |
EP1219646B1 (de) | 2005-11-16 |
DE50108076D1 (de) | 2005-12-22 |
ATE310030T1 (de) | 2005-12-15 |
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